JPH0798642B2 - Heat exchange reforming method and reactor - Google Patents

Description

The present invention relates to steam reforming of hydrocarbons in the presence of a catalyst (stea).
m reforming of hydrocarbons) and a reactor for carrying out this method. In particular, the present invention provides a method of supplying heat from a reformed gas product stream to a portion of the heat required for an endothermic reforming reaction that occurs in the process gas by indirect heat exchange between the product stream and the process gas. It is about.

[Problems to be solved by conventional techniques and inventions]

The endothermic reaction produced by the method for steam hydrocarbon reforming can be described by the following reaction equation.

_{(1) CH 4 + H 2} OCO + 3H 2 (-ΔH ° 298 = -49.3kcal / mole) (2 ) CH 4 + 2H 2 OCO 2 + 4H 2 (-ΔH ° 298 = -39.4kcal / mole) corresponding reaction equation, It can be established for steam reforming of hydrocarbons higher than methane. These steam reforming reactions occur in the treated gas consisting of steam and hydrocarbons that pass through the steam reforming catalyst under steam reforming conditions. The heat required for the endothermic reaction is usually supplied by combustion in the radiant furnace chamber. In the radiant furnace chamber, a catalyst is placed in a vertical tube that penetrates the furnace material.

It is well known to utilize the heat of the reformate gas product stream as a partial source of heat. Such a method is described in US Pat.
No. 9,017. According to the method described in this publication, the first part of the process gas undergoes steam hydrocarbon reforming in a normal radiant chamber while the second part of the process gas undergoes steam reforming by indirect heat exchange with the product stream. . The two parts of the process gas then merge and undergo another steam hydrocarbon reforming by a secondary reforming process in the presence of air, supplying heat from the internal combustion of the process gas. The product stream from the secondary reforming process acts as a heat exchange medium to heat the second portion of the process gas.

It is an object of the present invention to provide a steam hydrocarbon reforming process which more economically utilizes the heat from the hot flue gas produced by combustion in the burner as well as the heat from the product stream.

Another object of the invention is to provide a reactor for carrying out the process.

[Means for solving problems]

Accordingly, the present invention forms a feed stream consisting of a hydrocarbon feed and steam and converts the feed stream into a hydrogen-rich product stream using the feed stream as a process gas under a steam reforming condition for a predetermined amount of steam. The present invention relates to a steam hydrocarbon reforming method carried out by passing it through a reforming catalyst. According to the method of the present invention, the heat required for the endothermic reaction occurring in the processing gas and the heating of the processing gas is supplied by the following two different means.

(A) While the treated gas is passing through the first portion of the steam reforming catalyst, which constitutes 25% to 75% of the total amount of catalyst, a moderately hot flue gas as described below.
Heat is partly supplied from s) and the product stream.

(B) While the process gas subsequently passes through the final part of the steam reforming catalyst, which constitutes the balance of the total amount of the catalyst, heat is supplied from the hot flue gas produced by the combustion of the fluid fuel, whereby heat The flue gas is cooled to form a hot flue gas as described in (a) above.

An essential feature of the process of the invention relates to the supply of heat necessary for the endothermic reaction. We have found a more economical way to supply the heat required for the endothermic reaction by indirect heat exchange utilizing the heat from the product stream together with the heat from the hot flue gas. According to this method, heat exchange is achieved by carrying out the method of the invention. According to the method of the present invention, the hot flue gas and the product stream that supply heat to the process gas in step (a) above are separately and inversely in contact with the process gas during step (a) in indirect heat exchange contact. However, the hot flue gas that supplies heat to the process gas in step (b) above passes in the same direction in indirect heat exchange contact with the process gas to form a product stream during step (b). To do. The method of the present invention will be described in more detail below. However, in order to provide a basis for a better understanding of the problems associated with the present invention,
Other features of the method of the invention will first be briefly described. These other features relate to steam reforming conditions. Steam reforming conditions are generally obsolete in the process of the present invention and in conventional steam reforming processes. These trivial steam reforming conditions are described below.

The hydrocarbon feed forming the feed stream for the process of the present invention may be any of the hydrocarbons, hydrocarbon fractions or hydrocarbon mixtures commonly used as feeds for steam hydrocarbon reforming. Good. Typical feeds are various naphtha distillates such as natural gas, refinery off-gases, liquefied petroleum gas, and light petroleum distillates. The hydrocarbon feed must be desulfurized in order to be suitable as a feed for steam reforming. During the desulfurization, the total content of hydrocarbon sulfur is reduced to less than 1wt.ppm.

When the feed stream as process gas contacts the steam reforming catalyst,
A certain amount of steam is added to the hydrocarbon feed to provide a steam-to-carbon ratio of the feed stream that is large enough to prevent carbon formation. Hereinafter, the ratio of vapor to carbon will be expressed as the number of vapor molecules per carbon atom. Normal,
The minimum steam to carbon ratio is 1.1. However, in order to obtain a reliable conversion of hydrocarbons to hydrogen and carbon monoxide, the steam to carbon ratio is generally 1.5 to 7.0, preferably 2.0 to 4.5. In some cases carbon dioxide may be added with the steam. In that case, the steam to carbon ratio will be adjusted also taking into account the presence of carbon dioxide.

The steam reforming catalyst for the process of the present invention may be any conventional steam reforming catalyst used in conventional steam reforming processes. Such catalytically active component is typically metallic nickel. Nickel is deposited on the ceramic carrier material. Typical of carrier materials are alumina, spinel, magnesia, alumina-silica, and many other oxide refractories and mixtures or combinations of oxide refractories. It is well known to add promoters to reforming catalysts in order to obtain improved properties for specific purposes.
Such promoters include alkali and alkaline earth metal oxides.

The steam reforming reaction occurring in the treated gas starts at a temperature of 350 ° C. or higher in a state of contact with the steam reforming catalyst. The temperature of the feed stream at the catalyst inlet is generally 350-550 ° C, preferably 400-475 ° C. Under certain circumstances, it is preferred to heat the feed stream to about 600 ° C at the catalyst inlet. However, in order to obtain the desired degree of conversion of hydrocarbons to hydrogen and carbon monoxide, the temperature of the process gas must be gradually increased while it passes through the catalyst. Usually, the processing gas is 750 to 950 ° C, preferably 80
Leave the catalyst as a product stream at 0-900 ° C. Therefore, the endothermic reaction and raising the temperature of the process gas from the temperature at the inlet of the feed stream of 350-600 ° C. to the temperature of the outlet of the product stream at 750-950 ° C. require a partial supply of heat. To be done. For this purpose, the steam reforming catalyst must be placed in multiple compartments. These compartments are suitable for receiving the required heat by heat transfer through the compartment walls.

The amount of catalyst required for a steam reforming process is usually determined according to the following two criteria. (1) The amount of catalyst must be sufficient to ensure the residence time of the process gas required for the desired conversion. (2) The amount of catalyst must be such that it fills the catalyst compartment with a sufficient outer area required for all the heat transfer necessary for the endothermic reaction and heating of the process gas. Since most steam reforming catalysts have high activity, criterion (2) is usually determined for the choice of catalyst amount. The relationship between the amount of catalyst and the amount of process gas passing through the catalyst is usually expressed as the space velocity with respect to C ₁ hydrocarbon Nm ³ per m ³ of catalyst amount per hour. Here, C ₁ hydrocarbon means methane with the addition of some higher hydrocarbons expressed as the equivalent of methane. For steam reforming processes, the space velocity is typically 100-4000, preferably 200-2000. However, other considerations suggest high or low space velocities. For economic reasons, steam reforming processes are typically carried out at high pressures such as 2-45 bar. Within this range, the operating pressure can be selected according to the pressure at which the product stream is utilized or undergoes further treatment, for example 15-30 bar.

As mentioned above, an essential feature of the method of the invention relates to the supply of heat. This heat is first used in the endothermic reaction that occurs while the process gas passes through the steam reforming catalyst. Further, some heat is used to heat the process gas from the temperature of the feed stream at the inlet of the catalyst to the temperature of the product stream at the outlet of the catalyst. The novel method for supplying this heat is described in detail below.

Some of the heat required is obtained from the combustion of the fluid fuel and another is from the product stream. With the method of the present invention, a more economical utilization can be achieved by combining the heat from these two sources.

The present invention further provides a reactor for carrying out the steam hydrocarbon reforming process. This reactor utilizes a method of supplying heat to an endothermic reaction and is suitable for heating the process gas provided by the method of the present invention.

Accordingly, the present invention forms a feed stream consisting of a hydrocarbon feed and steam and converts the feed stream into a hydrogen-rich product stream using the feed stream as a process gas under steam reforming conditions under steam reforming conditions. The present invention provides a reactor for a steam hydrocarbon reforming process carried out by passing it through a catalyst. This reactor of the present invention comprises a removable lid, a pressure cylinder with an inlet and an outlet as described below, and comprises the following items:

(A) A catalyst compartment for holding a predetermined amount of steam reforming catalyst, which indirectly supplies heat required for heating the treatment gas and an endothermic reaction generated in the treatment gas when the treatment gas passes through the compartment. A catalytic compartment suitable for being received through the compartment wall by heat exchange.

(B) The feed stream is passed from the inlet through the pressure cylinder to the catalyst compartment and to the first part which constitutes 25-75% of the total amount of catalyst as process gas and further constitutes the balance of the total amount of catalyst. A flow path for passing to the final part.

(C) from the final portion of the catalyst to the compartment in indirect heat exchange contact with the product stream in an indirect heat exchange contact with the compartment holding the first portion of the catalyst to supply heat from the product stream to the process gas passing through the compartment. A flow path for passing the product flow to the outlet passing through the pressure cylinder.

(D) Burner for generating hot flue gas by combustion.

(E) A hot flue from a burner for cooling the hot flue gas to form a hot flue gas by supplying heat from the hot flue gas to the process gas passing through the compartment. A flow path for passing the gas in indirect heat exchange contact in the same direction as the process gas passing through the portion of the compartment holding the final portion of the catalyst.

(F) cooling the Japanese flue gas to form a cooled flue gas by supplying heat from the Japanese flue gas to the process gas passing through the compartment,
A flow path for passing the hot flue gas in an indirect heat exchange contact in a direction opposite to the process gas flow passing through the compartment holding the first portion of the catalyst.

(G) A flow path for passing cooling flue gas to an outlet through the pressure cylinder.

In a preferred embodiment of the reactor, a flow path for passing the product stream from the second catalyst compartment in indirect heat exchange contact with the process gas passing through the first catalyst compartment is provided with a product stream from the first catalyst compartment. It is adapted and positioned to flow in a direction opposite to the process gas passing through the chamber. This transfers as much heat as possible from the product stream to the process gas before the product gas leaves the reactor.

In a similar preferred embodiment of the reactor, a flue gas is first passed through indirect heat exchange contact with the process gas stream in the second catalyst compartment and further with the process gas stream in the first catalyst compartment. The flow path allows the hot flue gas to flow in the same direction as the process gas flow passing through the second catalyst compartment, and the hot flue gas in the opposite direction to the process gas flow passing through the first catalyst compartment. Adapted and positioned to flush. This transfers as much heat as possible from the flue gas to the process gas before it leaves the reactor. Not only is reverse flow heat exchange not suitable due to difficult control, uneven temperature distribution and unacceptable high material temperature, but also co-flow heat exchange is acceptable from an economic perspective. Not suitable as it creates an impossible high flue gas temperature.

The heat exchange reforming method and reactor of the present invention are suitable for producing a relatively small amount of hydrogen. One example is its unique use in remote natural gas producing areas. Another example is the fulfillment of the concomitant need for hydrogen, for example, to generate electricity by a fuel cell or some other power device. The atmosphere application makes it possible to limit energy consumption and reduce the demand for heat exchange through external attachments.

Furthermore, the method and reactor of the present invention may be used in large numbers in individual locations to accommodate different consumption of hydrogen, and in any event, the method and reactor of the present invention may be used in the power generation and chemical industries. It should be used. In all of these applications, the small size and the small amount of energy to be applied facilitates start-up, which allows the reactor of the present invention, for example, even when hydrogen is immediately needed for power generation. It can be started immediately.

The principle of the preferred embodiment of the method of the present invention will be briefly described based on the diagram of FIG.

Feed stream 10 passes as process gas 11 through a first portion 40 of the catalyst and further through a second portion 42 of the catalyst. Process gas 11 leaves second portion 42 of the catalyst as product stream 12. The hot flue gas 13 from the burner is in indirect heat exchange contact with the process gas 11 in the same direction as the process gas 11 passing through the second portion 42 of the catalyst.
At 61 passes along the second portion 42 of the catalyst. By being cooled during this indirect heat exchange, the hot flue gas 13 is endothermic reaction occurring in the process gas 11 passing through the second portion 42 of the catalyst and heating the process gas 11 to the temperature of the product stream 12. Supply the required heat. This cools the hot flue gas 13 and forms the hot flue gas 14.

The hot flue gas 14, after supplying heat to the second portion 42 of the catalyst, is in the opposite direction to the treatment gas 11 passing through the first portion 40 of the catalyst and in the indirect heat exchange catalyst state 62 with the treatment gas 11 of the catalyst. Pass along the first portion 40. By further cooling with this indirect heat exchange, the hot flue gas 14 causes an endothermic reaction to occur in the processing gas 11 passing through the first portion 40 of the catalyst and the temperature of the processing gas 11 at the outlet of the first portion 40 of the catalyst. Provides some of the heat needed to heat up. This cools the hot flue gas 14 to form the cooled flue gas 15. The balance of the required heat is supplied from the product stream 12, which, like the hot flue gas 14, is in the opposite direction of the process gas 11 and in the indirect heat exchange contact 63 with the process gas 11 and the catalyst no. Pass along a portion 40.

The new method of top-air heating, which supplies heat to the endothermic reaction that takes place as the process gas passes through the catalyst, is quite different from the known methods. However, maintaining steam reforming conditions for the method of the present invention is and is within the same range as is applied to known steam reforming processes based on external heating. These steam reforming conditions are as described above.

Further, specific examples of the reactor of the present invention are shown in the drawings.
FIG. 2 is a longitudinal sectional view of the reactor in the direction of its vertical axis. FIG. 3 is a horizontal cross-sectional view of the reactor. The reactor consists of a pressure lid 21, a pressure cylinder 20 with an inlet and an outlet, as described below. A catalyst basket 22 and a burner 23 are housed in the pressure cylinder 20.

A heat insulating material 24 is provided inside the pressure cylinder 20 and the lid 21. When the lid 21 is removed, the pressure cylinder 20 has an opening at its upper end of sufficient inner diameter to facilitate the attachment and removal of the catalyst basket 22. The bottom of the pressure cylinder 20 has a head for a burner 23.

A burner 23 is attached to the ostium, is fixed to the pressure cylinder 20, and is engaged with the pressure cylinder 20 in a pressure-tight manner. The burner 23 comprises a combustion head 25 and a ceramic tube 26 forming a combustion chamber 27. The ceramic tube 26 extends upward without engaging the catalyst basket 22.

The catalyst basket 22 is composed of a number of concentrically positioned plates which, with suitable walls, tubes, plates and baffles, feed stream 10, process gas 11, product stream 12 and flue gas 13, It forms the annular catalyst compartments and channels for 14,15.

The reactor described above is conditioned for two parts of the catalyst.
A first portion 40 of the catalyst is contained within an outer annular catalyst compartment 41. A second portion 42 of the catalyst is contained within the inner annular catalyst compartment 43. The inlet 44 for the feed stream 10 is located at the upper end of the pressure cylinder 20. Through these inlets, the feed stream 10 enters the top head 45 and further passes through the outer annular catalyst compartment 41 as process gas 11. The processing gas 11 passes from the bottom of the outer annular catalyst compartment 41 through a number of pipes 46 and reaches an inner annular flow passage 47 for further passing through the inner annular catalyst compartment 43. The product stream 12 from the inner annular catalyst compartment 43 is collected in the semi-annular space 48, from which it further passes through the outer annular channel 49 to reach the outlet 50.

The flow path for the flue gas from the burner 23 consists of an inner annular flue gas duct 51, the hot flue gas 13 from the combustion chamber 27 passing through that gas duct 51 to the bottom head 52 and further the hot smoke. It passes through the outer annular flue gas duct 53 as flue gas 14 and reaches the outlet 54 as cooling flue gas 15.

The inner annular flue gas duct 51 is arranged to provide indirect heat exchange for transferring heat from the hot flue gas 13 to the process gas 11 in the inner annular catalyst compartment 43. Similarly, the outer annular flue gas duct 53 is arranged to provide indirect heat exchange for transferring heat from the hot flue gas 14 to the process gas 11 in the outer annular catalyst compartment 41. To further transfer heat, the outer annular channel 49 is arranged to provide indirect heat exchange for transferring heat from the product stream 12 to the process gas 11 in the outer annular catalyst compartment 41. .

In order to obtain the correct function of the reactor, it is provided with equipment capable of substantially preventing heat from being transferred to the annular thin plate that separates the outer annular passage 49 and the inner annular passage 47. Similarly, there is a facility that can substantially prevent heat from being transferred from the processing gas 11 in the inner annular flow passage 47 to the processing gas 11 in the inner annular catalyst compartment 43 through the wall of the catalyst compartment 43. There is.

The details of the means for providing the indirect heat exchange required by the above description and preventing heat transfer are neither described nor shown in the drawings. However, such means are well known in the art.

〔Example〕

This example illustrates how particular aspects of the method of the invention can be performed. This example describes dynamic material, heat transfer material for applicable steam reforming catalyst,
And other sources of information relevant to conventional methods of steam hydrocarbon reforming, based on operational data obtained.
This state of the process of the invention was obtained with the reactor shown in the drawings and is described in detail below with respect to FIGS. 2 and 3. The operation materials are listed in Tables 1 and 2. In Table 1, the various gas stream components, pressures, and temperatures are associated with the various locations capitalized as shown in FIG.

Two steam reforming catalysts are used in this example.
Both catalysts are commercially available Handle Topse (Ha
ldor Tops φe) catalyst. Of this, 0.54 m ^{3 of the} catalyst called RKNR was used as the first portion 40 and the outer annular catalyst compartment 41
Put the catalyst called R-67 in the second part by 0.30m ³
42 was placed in the inner annular catalyst compartment 43.

Feed stream 10 is 248 Nm ³ / h of natural gas (95.06 mole% CH ₄ , 3.06
mole% C ₂ H ₆ , 0.46mole% C ₃ H ₈ , 0.22mole% C ₄ H ₁₀ , 0.46m
ole% N ₂ , 0.74mole% CO ₂ ) and 623 kg / h of steam. This amount of natural gas is 256 Nm ³ as shown above.
C ₁ hydrocarbons and air velocities equal to 305. This corresponds to a steam to carbon ratio of 3.0 as indicated above. Feed stream 10 is heated to 427 ° C and is inlet at a pressure of 5.85 kg / cm ² g.
After passing through 44, the catalyst contained in the catalyst compartments 41 and 43 is passed as the processing gas 11.

The process gas 11 has a first portion 40 of the catalyst in an outer annular catalyst compartment 41.
Process gas 11 receives a total calorific value of 414,400 kcal / h. This total heat is 158,200 kcl / h fuel from the product stream 12 passing through the outer annular flue 49 and 256,200 kcal / h from the hot flue gas 14 passing through the outer annular flue gas duct 53.
It is divided into the heat quantity of h. This heat is used for the endothermic reaction corresponding to 56.34% methane conversion and for heating the process gas to a temperature of 654 ° C. at the outlet of the outer annular catalyst compartment 41.

At the inlet of the inner annular catalyst compartment 43, the temperature of the processing gas 11 rises to 664 ° C. While the process gas 11 further passes through the second portion 42 of the catalyst in the inner annular catalyst compartment 43, the process gas 11 passes through the inner annular flue gas duct 51 and the hot flue gas.
Further receives heat of 13 to 312,000 kcal / h. This amount of heat is used for the endothermic reaction corresponding to another methane conversion of 37.01% and for heating the process gas 11 to a temperature of 805 ° C. at the outlet of the inner annular catalyst compartment 43. This processing gas 11
It is rich in hydrogen formed by 93.35% total methane conversion and passes through outer annular channel 49 as product stream 12. In the outer annular channel 49, the product stream 12 provides heat as described above, thereby cooling to a temperature of 537 ° C.

The hot flue gas 13 is produced in the combustion chamber 27 at a pressure of 3.46 kg / cm ² g by combustion of 417 Nm ³ / h of product gas (after removal of water) with 736 Nm ³ / h of air. Exit 54 for generated gas
740 Nm ³ / h of cooling flue gas recovered from is added. This recovery serves the purpose of lowering the temperature of the hot flue gas to 1370 ° C. before it contacts the inner annular catalyst compartment 43. As mentioned above, the hot flue gas 13 in an amount of 1775 Nm ³ / h passes through the inner annular flue gas duct 51, whereby it is cooled to 952 ° C. and the hot flue gas 14
And passing through the outer annular flue gas duct 53, the cooled flue gas 15 is cooled to a temperature of 587 ° C. as it leaves the reactor through the outlet 54. As mentioned above, a part of the cooling flue gas 15 equivalent to 41.65% is burner 2
Recovered to 3.

As is apparent from Table 1 below, cooling flue gas 15 and product stream 12 will leave the reactor at temperatures of 587 ° C and 537 ° C, respectively. In a typical reformer, the temperature at the flue gas outlet is about 1000 ° C and the temperature at the product gas outlet is about 800 ° C. Therefore, a normal reforming furnace requires a large-scale heat recovery device in order to obtain reliable heat economy.

[Brief description of drawings]

FIG. 1 is a diagram of the method of the present invention, FIG. 2 is a vertical cross-sectional view taken along the vertical axis in the side surface of an embodiment of the reactor of the present invention, and FIG. 3 is the reactor shown in FIG. It is a horizontal cross-sectional view of. 10 …… Supply flow, 11 …… Process gas 12 …… Production flow, 13 …… Hot flue gas 14 …… Wash flue gas 15 …… Cooling flue gas 20 …… Pressure cylinder, 21 …… Lid 23 ...... Burner, 27 ...... Combustion chamber 40,42 …… Catalyst 41,43 …… Catalyst compartment 44 …… Inlet, 50,54 …… Outlet 45,46,47,48,49,50,51,52, 53 ... Channel

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Claims (2)

[Claims] Claims: 1. A feed stream consisting of steam and one or more hydrocarbons is passed through a predetermined amount of steam reforming catalyst as a processing gas in a steam reforming state and under the external supply of heat to produce hydrogen. A method for steam reforming in a hydrocarbon reforming reactor forming a rich product stream, comprising: (a) passing the treated gas through a first portion of a steam reforming catalyst which constitutes 25-75% of the total amount of catalyst. The heat required for the endothermic reaction occurring in the process gas and the heating of the process gas is partly derived from the hot flue gas and partly from the product stream as described in (b) below. And (b) passing the treatment gas partially reformed in step (a) through the remaining portion of the steam reforming catalyst to generate heat necessary for another endothermic reaction and heating of the treatment gas. , Obtained by the hot flue gas produced by the combustion of the fluid fuel, which cools the hot flue gas in stages ( ) Is used to form the hot flue gas, and the hot flue gas and the product stream supply heat in step (a) and pass through step (a). The flue gas that passes simultaneously and separately to the process gas in the opposite direction of the process gas flow in indirect heat exchange contact and that supplies heat to the process gas in step (b) passes through step (b). A steam reforming method, wherein a process gas passing therethrough to form a product flow is passed in an indirect heat exchange contact state in the same direction as the process gas flow. 2. A hydrogen-containing hydrogen gas is produced by passing a feed stream consisting of steam and one or more hydrocarbons as a processing gas in a steam reforming state and under the external supply of heat to a predetermined amount of a steam reforming catalyst. A method for steam reforming in a hydrocarbon reforming reactor forming a rich product stream, comprising: (a) passing the treated gas through a first portion of a steam reforming catalyst which constitutes 25-75% of the total amount of catalyst. The heat required for the endothermic reaction occurring in the process gas and the heating of the process gas is partly derived from the hot flue gas and partly from the product stream as described in (b) below. And (b) passing the treatment gas partially reformed in step (a) through the remaining portion of the steam reforming catalyst to generate heat necessary for another endothermic reaction and heating of the treatment gas. , Obtained by the hot flue gas produced by the combustion of the fluid fuel, which cools the hot flue gas in stages ( ) Is used to form the hot flue gas, and the hot flue gas and the product stream supply heat in step (a) and pass through step (a). The flue gas that passes simultaneously and separately to the process gas in the opposite direction of the process gas flow in indirect heat exchange contact and that supplies heat to the process gas in step (b) passes through step (b). A reactor for carrying out a steam reforming method, characterized in that a process gas passing therethrough to form a product stream is passed in an indirect heat exchange contact state in the same direction as the process gas flow, Pressure cylinder (20) with removable lid (21), burner (23), combustion chamber (27), feed stream (10) to process gas (1
1) as means) for passing from at least one inlet (44) through the reforming catalyst to at least one outlet (50), and means for transferring heat to the process gas (11) by indirect heat exchange. (I) has a first catalyst compartment (41) and a second catalyst compartment (43), these compartments comprising a portion of the catalyst which constitutes 25-75% of the total amount of the catalyst and the remainder of the catalyst. And is adapted to receive heat required for heating the processing gas (11) and for an endothermic reaction that occurs in the processing gas when the processing gas passes through the catalyst through the wall of the compartment, (ii) A flow path for passing the processing gas (11) from the inlet (44) to the outlet (50) through the first catalyst compartment (41) and the second catalyst compartment (43), and (iii) the first catalyst Process gas (1) passing through the compartment (41)
Suitable for passing the product stream (12) from the second catalyst compartment (43) to the outlet (50) in indirect heat exchange contact with (1), and the process gas (1) passing through the first catalyst compartment (41). A portion of the flow path of (ii) adapted and positioned to flow the product flow (12) in the opposite direction to (11), and (iv) flue gas from the combustion chamber (27) First, as the hot flue gas (13), the process gas (11) in the second catalyst compartment (43)
To the process gas (11) in the first catalyst compartment (41) as the flue gas (14) in the indirect heat exchange contact state, and finally to the flue gas. Is a cooling flue gas (15) discharged from at least one outlet (54), the hot flue gas (13) passing through the second catalyst compartment (43) 13) and is adapted and positioned to flow the hot flue gas (14) in the opposite direction to the process gas (11) passing through the first catalyst compartment (41). A reactor having an open flow path.